Process for converting petroleum oil



`April 12, 1932.

J. D. sl-:GUY

PROCESS FOR CONVERTING PETROLEUM IL Original Filed March 16. 1923 15 elevational vsa f Patented Apr. 12,1932

UNITED STATESl PATENT OFFICE JEAN D. SEGUY, OF CHICAGO, ILLINOIS, ASSIGNOR T THE UNIVERSAL OIL PRODUCTS COMPANY, OF CHICAGO, ILLINOIS, A CORPORATION OF SOUTH DAKOTA rnocnss non comerme PETROLEUM oir.

Application filed March 16, 1923, Serial No. 625,457.

This invention relates to improvements in a process for converting petroleum oil a nd refers more particularly to the destructive distillation of relatively high boiling point oils to produce oils ofv a lower boiling point having the characteristics of. gasoline.

Among the objects of the invention are to provide a process in which the oil is treated, first, to remove the more easily cracked prod- 1o ucts by pressure distillation, and subsequentp ly the unvaporized and reflux portions are directed toa second stage of treatment where'- ina further conversion takes place.

The single ligure is a diagrammatic side view ofthe apparatus suitable for carrying out my process.

Referring to the drawing, the oil to be treated is introduced from any convenient extraneous source through the line 1 and is charged by means of the pump 2 through va line 3 which has interposed therein the revheating coils 4 and 5 positioned in the ues of the furnaces 6 and 7 respectively. The discharge end of the coil 5 connects with the heating coil 8 positioned in the furnace 7. This heating coil is connected by means of a "transfer line 9 controlled by a valve 10 to a vaporizing or expansion chamber` 11 which is equippedv 'th try-cocks'12 for ascertaining the liquid level maintained therein,4 andv residuum draw-olf lines 13 controlled by valves 14. 1

To removethe vapors 'from the chamber a vapor line 15 controlled by a valve 16 is connected into the top ofthe chamber and communicates with the refluxing tower 17 in which are positioned baling members or pans 18 for the purpose ofcausing the vapors to pass therethrough in a circuitous travel and at the saine time offering the liquid reiuxing agent, introduced into the top ofthe column through the spray'pipe 19, the opportunity of intermingling more thoroughly. with the vapors rising throughthe column. The dephlegmated vapors passl from the top of the column .through the line 20 and are subjected to a inal condensing 4action in the condenser coil 421 after which'they are collected as liquid 0 the latter being equipped with a gas rehe distillate in the receiver 22 Renewed April 15, 1929.

pipe 23'a pressure gauge'24, liquid level gauge 25, and a liquid draw-olf valve 26. The condensate separated out in the Vdephlegmating column collects in the lower leg of the column desi ated 'as 17 a and may be drawn off through the line 27 which is connected to the pipe 281 communicat'ng with the residuum lines 13, or, it ma be directed through the cooling coil 2 9 an charged by means of the ump 30 through the line 31 back into the top ofthe dephleginator or portions recycled in this manner and the rest of the reflux permitted to continue to the pipe 28 through which itis introduced into the heating coil 32 positioned in the furnace 6.

A further disposition of the reflux con? densate separated out in the column 17 is through the pipe 33 and into the top of the refluxing column 34 through the spray pipe 35. In order to do this it is necessary to close the valve .36 and open the valve 37, or by partiallyopening each'of the valves regulated quantities ofthe relux may be direct ed to the top of each of the dephlegmators for reluxin purposes. The cooling coil 29 75 is interpose in the return line to cool the re-A luxing medium in order that the pumping -vmechanism willnot be subjected to excessive.

temperature and also for the purpose of supplying a cooler medium to the top of the. dephlegmators. Y This cooling coil-may be cooled by'water or by circulating the',l raw oil about the hot coil'29 containi g the reflux condensate. In the drawing it is shown to be watercooled,; but *by diverting the charging line to circulate the raw oil bout this coil this heat could. l be conserved instead of being lost as it would be by water cooling.

The liquid oil drawn oif from the vaporiz- 9o\ ing chamber throu h the' residuum lines and also the reflux con ensate notrecycled to the top of the vdephlegmating columns, are combined in the pipe 28 and directed to the heating coil` 32 mounted in the furnace 6 whereL 95 they are subjected to temperature and presL4 sure conditions regulated to produce further l conversion. `This oil isof.a'-relativelyheiry'V nature, containintghconsiderable carbonaceous material. It is erefore essential 'thtfgtliejlj oil be circulated during its heattreatment at a relatively high velocity and that the temperature and pressures maintained thereon be carefully regulated.

f The oil after being heated is passed through transfer line 38 regulated by a valve 39 and is permitted to vaporize in the chamber 40 which is similar to the chamber 11.

. The vaporized oil constituents separated out in the chamber 40 rise through the vapor line 41 re ulated by a valve 42 and pass up through tie column 34 where they are subjected to a dephlegmating action. Passing off from the top of the dephlegmator 34 the vapors are directed through the line 43 to the condenser 44, subsequent to Which they are collected as distillate in the receiver 45 which is identical in construction to that shown at 22. The dephlegmation of the vapors in the column 34 is effected by recirculation of the condensate from the column 17 through the pump 30 and line 33. The vapors are also caused to follow a circuitous route through the tower due to the positioning of the pans 46 as obstructions or baliles.

The reflux products-separated out in the column 34 are collected in the lower leg thereof designated as 340, and are drawn oil", through the line 47 and mixed with the liquid oil drawn off from the first stage through pipe 28. It being, of course, understood that suitable check valves are provided in pipe 28 and line 47 as shown. These combined products are pumped by means of the pressure pump 48 through the line 49 to the inlet end of the heating coil 32 where-they are reheated. The chamber 40 is equipped with try-cocks 50 and residuum drawoi lines 51 controlled by valves 52.

A lead 53 regulated by a valve 54 is interposed between the line 28 and the pipe 3, by means of which the residual products may be recycled to the initial stage in place of introduction to t-he second stage oit' treatment or regulated quantities may be recycled to the initial stage, the remaining portions being retreated in the secondary stage as explained.

By means of a connecting lead 55 controlled by valve 56 and valves 57 and 58 in the lines 20 and 43 respectively, it is possible to combine portions of the vapors escaping from the separate refiuxing columns.

By treating the oil in its successive stages in lthis manner and by recycling the reflux condensate and utilizing the same as a refiuxing medium, together with the conserving of heat in the system by the preheating methods described, it is possible to relieve a charging` stock of considerably greater quantities of low boiling point oils than can be produced by a single stage cracking system in which the oil is circulated but once through thef'system and is treated but a single time for its lighter fractions. The recirculation of the 5 reflux condensate also effects a more complete By treating a Mid-Continent gas oil of approximately 32 Baum at temperatures ranging from 700 to 900 F. and pressures from 200 to 500 pounds per square inch, and subsequently treating the unvaporized portions, such as the residuum, and reliux condensate in a separate zone of treatment wherein temperatures and pressures may be regulated to produce the most eective conversion, a good quality distillate may be relieved in the initial stage and also in the secondary stage, producing considerably in excess of what could be separated by the conversion in the single stage. Distillates ranging from 50% to 70% of the charging stock and having comparatively satisfactory ranges of boiling points and gravity may be produced.

The process is preferably operated continuously, it being necessary only to shut down when the carbon accumulation in the expansion chambers becomes objectionable.

I claim as my invention:

1. A process for converting hydrocarbon oil consisting in heating and vaporizing the oil in a primary stage under a substantial pressure, subjecting the evolved vapors to a dephlegmating action, condensing and collecting the dephlegmated vapors, directing the reflux condensate and unvaporized oil constituents resulting from the treatment in said primary stage to a secondary stage of treatment and there subjecting the combined products to heat and pressure conditions to produce further conversion, dephlegmating and condensing the vapors evolved in the secondary conversion stage in returning the reiux condensate produced in the secondary stage for retreatment in said secondary stage, and in employing reiux condensate produced in the primary stage as a reuxing medium in both stages. i

2. A process for converting hydrocarbon oil consisting in heating and vaporizing the oil under a substantial pressure, subjecting the evolved vapors to a dephlegmatin action, condensing and collecting the dep legmated vapors, directing reflux condensate and unvaporized oil constituents to a secondary stage of treatment and there subjecting the combined products to heat and pressure conditions to produce further conversion, dephlegmating and condensing the vapors evolved in the secondary conversion stage, recycling selected portions of the re fiux condensate removed from the initial dephlegmating stage to the top of the initial and secondary stages of dephlegmation and maintaining regulated pressure upon the system during treatment.

3. A process of treating hydrocarbon Oil consisting in passin the oil throu h an initial heating zonev w erein it is su jected to a conversion temperature while maintained under a substantial pressure2 in discharging the oil from the heating zone into an enlarge conversion chamber wherein substantial vaporization occurs, passing the evolved vapors to a dephlegmator, in condenslng the dephlegmated vapors and in collecting the .resulting distillate, in combining portions of the reflux condensate formed .in s aid dephlegmator with unvaporized 011 wlthdrawn from saidgconversion chamber, 1n d1- recting portions of said combined reflux conindependent conversion chamber, in condensing and collecting the dephlegmatedvapors,`

in returning the reiux condensate resulting from such dephlegmation to said secondary heating zone to b e passed therethrough together with said reflux condensate and unvaporized raw oil from the primary zone for retreatment.

'4. A process of treating hydrocarbon oil consisting in continuously passing the` oil through an initial heating zone wherein the oil is subjected to a conversion temperature while maintained under a substantial pres-I sure, in discharging the oil from said zone '1nto an enlarged conversion chamber, 1n

dephlegmating the evolved vapors, in condensing the dephlegmated vapors, in collecting the resulting distillate, in passing reflux condensate,resulting from such dephlegmation together with the unvaporized oil withdrawn from said conversionchamber under an applied pressure to a secondary heating z one wherein the oil is subjected to condit1ons of temperature and pressure to roduce -a further cracking thereof, in discharging the heated oil from said secondary heating zone, into an independent conversion chamber, in passing the vapors evolved in said second conversion chamber t0 a dephlegmator, in introducing into said dephlegmator reflux condensate produced from the dephlegmation of the vapors evolved in the initial conversion chamber, to act as adephlegmatin medium, in condensing the dephlegmate vapors, in collecting the `resulting distillate and in returning the reflux condensate from said dephlegmator to said secondary heating zone.

JEAN D. sueur. 

